Patent GB-600777-A (GB)
Title: Hydrogenation of organic compounds
IPC: C10G45/56
Filed: 1945-05-30
Abstract: Organic compounds particularly naphthas and butene polymers, are hydrogenated in vapour form under a pressure of at least 50 lbs. per sq. in. by passing in admixture with hydrogen through a hydrogenation zone containing a subdivided hydrogenation catalyst, the velocity of the gases being controlled so as to maintain the catalyst in the form of a fixed fluidized bed and the reaction temperatures being controlled by heat exchange with a cooling medium, while catalyst separated from the reaction products is returned direct to the hydrogenation chamber.  The feed, e.g. a low-boiling naphtha containing unsaturated constituents, is introduced at 10 and may pass through a heat exchanger 13 and furnace 33.  The catalyst, e.g. a mixture of tungsten and nickel sulphides may be withdrawn from the reactor 19 through line 22 via a cooler 24, or through line 25, and mix with the feed in line 18.  A hydrogen-containing gas enters at 27 and passes through line 31 to join the feed.  The pressure in the reactor may be 50-1000, preferably 100-200 lbs. per sq. in. and the temperature 400-600 DEG  F.  Catalyst entrained in the reaction products is removed by the <PICT:0600777/III/1> cyclone separator 35, the gases are scrubbed with oil at 38, and pass via heat-exchanger 13 and condenser 45 to separator 46. Liquid products (some of which may be used in the scrubber 38) are removed at 67 and gaseous products may be washed with water at 50 to remove entrained catalyst, and then returned via line 48 to mix with the hydrogen feed.  The slurry of water and catalyst formed in vessel 54 is led to the reactor.  Fresh catalyst may be supplied to the system from a pressure hopper 69.  In a modification (Fig. 2, not shown), the catalyst is cooled by means of tubes containing a vaporizable liquid, e.g. water, arranged in the reactor, and the pressure in the tubes is automatically controlled according to the temperature of the reactor; also the liquid reaction product is scrubbed with water to remove suspended catalyst. Specifications 554,227, 558,879 and 600,776 are referred to.  The Specification as open to inspection under Sect. 91 states that the process may also be used for the hydrogenation of acids, aldehydes, ketones and alcohols.  This subject-matter does not appear in the Specification as accepted.ALSO:<PICT:0600777/IV(b)/1> Organic compounds, e.g. naphthas and butene polymers, are hydrogenated in vapour form under a pressure of at least 50 lbs. per sq. in. by passing in admixture with hydrogen through a hydrogenation zone containing a subdivided hydrogenation catalyst, the velocity of the gases being controlled so as to maintain the catalyst in the form of a fixed fluidized bed.  The feed, e.g. a low-boiling naphtha containing unsaturated constituents, is introduced at 10 and may pass through a heat-exchanger 13 and furnace 33.  The catalyst, e.g. a mixture of tungsten and nickel sulphides may be withdrawn from the reactor 19 through line 22 via a cooler 24, or through line 25, and mix with the feed in line 18.  A hydrogen-containing gas enters at 27 and passes through line 31 to join the feed.  The pressure in the reactor may be 50-1000, preferably 100-200 lbs. per sq. in., and the temperature 400-600 DEG  F.  Catalyst entrained in the reaction products is removed by the cyclone separator 35, the gases are scrubbed with oil at 38 and pass via heatexchanger 13 and condenser 45 to separator 46.  Liquid products (some of which may be used in the scrubber 38) are removed at 67 and gaseous products may be washed with water at 50 to remove entrained catalyst, and then returned via line 48 to mix with the hydrogen feed.  The slurry of water and catalyst formed in vessel 54 is led to the reactor.  Fresh catalyst may be supplied to the system from a pressure hopper 69.  In a modification (Fig. 2, not shown), the catalyst is cooled by means of tubes containing a vaporizable liquid, e.g. water, arranged in the reactor, and the pressure in the tubes is automatically controlled according to the temperature of the reactor; also the liquid reaction product is scrubbed with water to remove suspended catalyst. Specifications 554,227; 558,879 and 600,776, [both in Group III], are referred to.  The Specification as open to inspection under Sect. 91 states that the process may also be used for the hydrogenation of acids, aldehydes, ketones and alcohols.  This subject-matter does not appear in the Specification as accepted.